Reactive Membrane Process for the Removal of Vapor Phase Contaminants

ABSTRACT

Generally, the present invention provides a method and apparatus for removing a vapor phase contaminant from a gas stream, thereby reducing the concentration of the vapor phase contaminant in the gas stream. In one embodiment, the present invention provides a method for removing a vapor phase contaminant from a gas stream, comprising contacting a gas stream comprising a vapor phase contaminant with a first side of a membrane; sorbing the vapor phase contaminant using the membrane; reacting the vapor phase contaminant into an reacted form of the vapor phase contaminant; transporting the reacted form of the vapor phase contaminant through the membrane to a second side of the membrane; contacting the second side of the membrane with a liquid; and dissolving the reacted form of the vapor phase contaminant into the liquid. Methods for making a membrane comprising a metal for use in the present invention is also described.

RELATED APPLICATION

This application is a divisional of U.S. application Ser. No.10/913,174, filed Aug. 5, 2004, which is incorporated by referenceherein in its entirety.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to a method and apparatus for removingvapor phase contaminants from a gas stream. More particularly, thepresent invention relates to a method and apparatus for the removal ofvapor phase contaminants from flue gases generated by a coal-firedboiler using a membrane.

2. Description of Related Art

Utility power plants are concerned about emissions of trace metals inlight of the 1990 Clean Air Act Amendment (CAAA) on air toxics (TitleIII). Special attention has been given to mercury (Hg) in terms of itsenvironmental release and impacts, and the Environmental ProtectionAgency (EPA) is closely scrutinizing sources that emit mercury. The EPAhas determined that utility power plants, and specifically coal-firedpower plants, are the major remaining source of mercury emissions intothe air. Mercury is present in flue gas generated by coal-fired powerplants in very low concentrations (<5 ppb) and forms a number ofvolatile compounds that are difficult to remove. Specially designed andcostly emissions-control systems are required to capture these traceamounts of volatile compounds effectively.

Several approaches have been adopted for removing mercury from gasstreams. The most common methods are often called “fixed-bed”techniques. In these systems, the gas containing mercury is passedthrough a bed consisting of sorbent particles held in place by variousstructures such as honeycombs, screens or fibers. A common sorbent isactivated carbon in powder form.

There are, however, several disadvantages of fixed bed systems. Gasstreams such as those from power plant coal combustion containsignificant fly ash that can plug the bed structures and, thus, the bedsneed to be removed frequently from operation for cleaning.Alternatively, these beds may be located downstream of a separateparticulate collector (see, for example, U.S. Pat. No. 5,409,522,entitled “Mercury Removal Apparatus and Method,” which is incorporatedby reference herein in its entirety). Particulate removal devices ensurethat components of the flue gas such as fly ash are removed before thegas passes over the mercury removal device. The beds will still need tobe taken off-line periodically for regeneration, thereby necessitating asecond bed that can remain on-line while the first one is regenerating.These beds also require significant space and are very difficult toretrofit into existing systems such as into the ductwork of power plantswithout major modifications.

In another process for removing mercury or other vapor phasecontaminants from a flue gas stream, a carbonaceous starting material isinjected into a gas duct upstream of a particulate collection device.The carbonaceous starting material is activated in-situ and adsorbs thecontaminants. The activated material having the adsorbed contaminants isthen collected in a particulate collection device. Such a process isdescribed in U.S. Pat. Nos. 6,451,094 and 6,558,454, both entitled“Method for Removal of Vapor Phase Contaminants From a Gas Stream byIn-Situ Activation of Carbon-Based Sorbents,” which are bothincorporated by reference herein in their entireties. However, the needto replenish the carbonaceous starting material and collect the spentactivated material in a particulate collection device creates extrasteps that consume additional resources.

In yet another process to remove mercury in a flue gas stream, goldand/or metals from Groups IA, IB, and III of the Periodic Table ofElements can be used as a sorbent to adsorb mercury, as described inU.S. Pat. No. 5,409,522, entitled “Mercury Removal Apparatus andMethod,” which is incorporated by reference herein in its entirety. Inthis process, mercury is adsorbed and amalgamated with the sorbent thatis disposed on a collection surface. The sorbent can be regenerated byapplying heat to the sorbent surface, thereby releasing themercury-containing compound. Even though the sorbent can be regeneratedto save costs, the regeneration process creates an extra step thatconsumes time and other resources to set up and maintain.

Elemental mercury is particularly difficult to remove by theseconventional methods. To address this difficulty, gold and/or othernoble metals may be used as a catalyst to convert elemental mercury(Hg(0)) into an oxidized form, such as mercury (II) chloride, sinceoxidized forms are easier to remove. Oxidation of mercury through goldand/or other noble metals is possible when handling flue gas streamscontaining at least 20 ppm HCl gas. The gold and/or noble metal may bedisposed on a catalyst bed supported by a screen in a duct. Such aprocess is described in U.S. Pat. No. 6,136,281, entitled “Method toControl Mercury Emissions from Exhaust Gases,” which is incorporated byreference herein in its entirety.

In view of the foregoing, there exists a need for an improved method andapparatus for removing vapor phase contaminants such as mercury from agas stream.

SUMMARY OF THE INVENTION

Generally, the present invention provides a method and apparatus forremoving a vapor phase contaminant from a gas stream, thereby reducingthe concentration of the vapor phase contaminant in the gas stream. Inone embodiment, the present invention provides a method for removing avapor phase contaminant from a gas stream, comprising contacting a gasstream comprising a vapor phase contaminant with a first side of amembrane; sorbing the vapor phase contaminant using the membrane;reacting the vapor phase contaminant into an reacted form of the vaporphase contaminant; transporting the reacted form of the vapor phasecontaminant through the membrane to a second side of the membrane;contacting the second side of the membrane with a liquid; and dissolvingthe reacted form of the vapor phase contaminant into the liquid. In someembodiments, the reaction comprises oxidation of the vapor phasecontaminant, such as mercury or sulfur oxides, including, for example,sulfur dioxide. In another embodiment, the reaction comprises reducingthe vapor phase contaminant, such as NO.

In another embodiment the present invention provides an apparatus forremoving a vapor phase contaminant from a gas stream flowing in a gasduct, comprising a membrane disposed within a gas duct and a containerconfigured to hold a liquid adjacent to a first side of the membrane.The membrane can be made of polymer, including perfluorinated polymerssuch as TEFLON® or NAFION®. The membrane may also comprise of a metalselected from a group consisting of gold, silver, palladium, platinum,copper, nickel and mixtures thereof. The membrane may also comprise of aGroup VI clement, such as selenium.

In yet another embodiment, the present invention provides a method forproducing a metallized membrane, comprising contacting a first side of apolymer membrane with a first solution comprising a metal; contacting asecond, opposite side of the polymer membrane with a second solutioncomprising a reducing solution; and passing the reducing solutionthrough the polymer membrane, thereby reducing the first solution anddepositing the metal on the first side of the polymer membrane.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a cross-sectional view of one embodiment of the presentinvention;

FIG. 2A is a plan view of the embodiment of a membrane unit of FIG. 1taken along line 2-2 of FIG. 1;

FIG. 2B is a plan view of another embodiment of a membrane unit;

FIG. 2C is a plan view of yet another embodiment of a membrane unit;

FIG. 3A is a flowchart of a method to produce a metallized membraneaccording to one embodiment of the present invention;

FIG. 3B is a perspective view of a tank used in the method of FIG. 3A;

FIG. 3C is a top view of a frame that may be used in connection with thetank of FIG. 3B;

FIG. 4 is a flowchart of a method to produce a metallized membraneaccording to another embodiment of the present invention; and

FIG. 5 is a flowchart of a method of vapor phase contaminant removalaccording to one embodiment of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

Generally, the present invention provides a method and apparatus forremoving a vapor phase contaminant or multiple vapor phase contaminantsfrom a gas stream, thereby reducing their concentration in the gasstream. In one embodiment, the present invention provides a method andapparatus for reducing the concentration of vapor phase contaminantssuch as mercury, sulfur oxides, including, for example, sulfur dioxide,and nitrogen oxides, such as NO, in a flue gas stream from a coal-firedpower plant boiler. Generally, the method and apparatus of the presentinvention utilize a membrane wherein the vapor phase contaminant issorbed by the membrane; reacted or chemically converted, if necessary,into a reacted or predetermined form, such as a soluble form;transported through the membrane to the opposite side of the membrane;and dissolved into a liquid stream in contact with that side of themembrane, wherein the liquid stream may be subsequently treated toremove the dissolved contaminant.

The following text in connection with the Figures describes variousembodiments of the present invention. It should be appreciated thatwhere the same numbers are used in different Figures, these numbersrefer to the same element or structure throughout. The followingdescription, however, is not intended to limit the scope of the presentinvention.

FIG. 1 is a cross-sectional view of one embodiment of the presentinvention. Specifically, FIG. 1 is a cross-sectional view of a membraneremoval system 100 disposed within a gas duct 110, wherein the gas flowis normal to the page. The membrane removal system 100 comprises aplurality of membrane units 120 that are held in place by a supportstructure 130. Each membrane unit 120 comprises a pair of membranes 140and a pair of end plates 240 (shown in FIG. 2) that form a liquid-tightregion 170 between each pair of membranes 140. This region 170 isconfigured to hold a liquid between the membranes 140 during operation,wherein the liquid may be stationary or may be flowing. In thisparticular embodiment, the membrane units 120 and the membranes 140 areoriented horizontally; however, they may also be oriented vertically. Ineither case, the membranes 140 are substantially flat and may extend forany desired length along the length of the duct 110 (i.e., the membranesextend in a direction normal to the page and in the same direction asthe gas flow through the duct 110). It should be appreciated that theoverall dimensions of the membrane 140 will dictate the total surfacearea of the membrane 140 available for contact with the gas stream thatflows over the membrane surface. Therefore, depending upon theparticular vapor phase contaminant to be removed and its concentration,the gas flow rate and other process conditions, such as temperature andhumidity, the overall size of the membrane 140 can be determined. Thespace between the membranes that defines the region 170 that holds theliquid is discussed below in connection with FIG. 5.

The support structure 130 is configured to hold the membranes 140 inplace and substantially flat during operation. Further, the supportstructure 130 may be configured to provide a liquid-tight seal along thelength of each of the membrane units 120 and at each of the ends of eachof the membrane units 120 so that the liquid held in the region 170between each pair of membranes 140 does not leak into the gas stream.Alternatively, each membrane unit 120 may be surrounded at its perimeterby a frame that is configured to hold each pair of membranes 140 inplace and that maintains a liquid-tight seal around the perimeter of themembrane unit 120. In this case, each membrane unit 120 may beseparately placed into the support structure 130, which may simply be arack configured to hold the desired number of membrane units 120 withthe desired spacing between each membrane unit 120.

Connected to the support structure 130 is a pair of tubes or pipes 180,181 that are configured, respectively, to deliver and remove a liquid toand from each region 170 between each pair of membranes 140. In oneembodiment, the pipes 180, 181 may each be connected to a correspondingheader 182 that is common to each region 170 between each pair ofmembranes 140. Alternatively, a separate pair of tubes or pipes thatconnect individually to each region 170 between each pair of membranesand that each extend outside of the duct 110 may be used (not shown).

These pipes 180, 181 extend outside of the duct 110 and may beseparately connected to external tanks (not shown): one tank forcollection of spent liquid from the membrane units 120 and a second tankholding regenerated or fresh liquid that is pumped to the region 170between each pair of membranes 140. The system for removing spent liquidfrom the membrane units 120 and for feeding fresh liquid to the membraneunits 120 may be controlled by various flow control electronics (notshown). For example, flow control techniques may be utilized to feedliquid at different rates to each of the membrane units 120, dependingupon the amount of vapor phase contaminant that is removed from the gasby each membrane unit 120.

It should be appreciated that the membrane removal system 100 shown inFIG. 1 is not drawn to scale. As discussed below, the membrane units 120may be much smaller in size relative to the diameter of the duct 110.For example, the thickness of each membrane unit 120 may besignificantly smaller than shown. As a result, any number of membraneunits 120 may be used or placed adjacent to one another in the membraneremoval system 100, depending upon the effect on the pressure drop ofthe gas flow through the duct 110. Additionally, the spacing betweeneach membrane unit 120 may be altered. For example, relatively moremembrane units 120 will result in less space between each of them,thereby increasing the pressure drop but providing a greater amount ofmembrane surface area available to contact the gas and sorb the vaporphase contaminant. Alternatively, where process conditions dictate agiven gas flow requirement, the number of membrane units used can bereduced. Moreover the length of each membrane may be increased tomaintain a given contact area with the gas, as opposed to increasing thenumber of membrane units in the duct. It should also be appreciated thatmultiple membrane removal systems 100, each having multiple membraneunits 120 may be placed within the duct 110 in series.

Specifically in the context of removing vapor phase contaminants,including, for example, mercury present in the flue gas of a coal-firedpower plant, it should be appreciated that the location of the membraneremoval system 100 within the duct 110 or along the flue gas path can bealtered. Depending on the vapor phase contaminant to be removed, thecomposition of the membrane and composition of the liquid in themembrane units 120, there may also be a temperature effect on thesorption of the vapor phase contaminant. As will be discussed below inconnection with mercury removal, gold-metallized membranes may be usedwith a solution of nitric acid as the liquid between each pair ofmembranes. In this case, the membrane removal system 100 should bepositioned where the ambient temperature is not much higher thanapproximately 200° F., such as downstream of a wet flue gasdesulfurization system if present. In one embodiment for mercuryremoval, the membrane removal system 100 would operate at an ambienttemperature range of approximately 100-150° F. It should be appreciatedthat the temperature of the gas should be taken into account whenselecting the membrane composition to ensure that the membrane iscapable of withstanding the gas temperature.

Furthermore, the placement of the membrane system 100 may also beinfluenced by the particulate loading or fly ash in the gas stream, suchas the flue gas from a coal-fired power plant boiler. For the membraneremoval system 100 to function as desired, the membrane surfaces shouldnot be overloaded with particulate. Therefore, the membrane removalsystem 100 should be placed in a location where the gas has a lowparticulate concentration, such as downstream of a particulatecollection device or a scrubber.

FIG. 2A is a plan view of the embodiment of a membrane unit of FIG. 1taken along line 2-2 of FIG. 1. FIG. 2 illustrates a single membraneunit 120 comprising a pair of membranes 140 and a liquid-tight region170 between them, where the flue gas stream 210 flows over and under themembranes 140. A pair of end plates 240 are shown, which are configuredto hold the membranes in place and to provide a liquid-tight seal at theends of the membrane unit 120. In this case, once the membrane unit 120is positioned within the support structure 130, that support structure130 provides a liquid-tight seal along the length of the membrane unit120. It should be appreciated that the end plates 240, while shown asflat, may be aerodynamically designed so as to minimize the disruptionof the gas flow upon impacting the membrane unit 120 and to maximize gascontact with the surfaces of the membranes 140. For example, the endplates 240 may be designed to effect an appropriate amount of gas flowturbulence to maximize contact between the bulk gas and the membranesurface as the gas passes over the membrane surface. As discussed above,a frame that extends about the entire perimeter of the membrane unit 120may alternatively be used to hold the membranes 140 in place in themembrane unit 120 and to provide a liquid-tight seal around the entiremembrane unit 120. It should be appreciated that any other structure ormaterial may be used to provide a liquid-tight seal around the perimeterof the region 170 between each pair of membranes 140, provided such iscompatible with the gas environment and the liquid to be held betweenthe membranes 140.

FIG. 2B is a plan view of another embodiment of a membrane unit. In thisembodiment, the membrane unit 190 comprises a pair of membranes 191 anda liquid-tight region 192 between them, in which the membranes 140 arefolded in an accordion-like fashion to provide additional contactsurface area. A pair of end plates 241 are used to hold the membranes191 in place and to provide a liquid-tight seal at the ends of themembrane unit 190. Similarly to the membrane unit described inconnection with FIG. 2A, this membrane unit 190 may also be used with aframe that provides a liquid-tight seal around its perimeter or may relyupon the support structure to provide a liquid-tight seal along itslength. This membrane unit 190 may be configured in a membrane removalsystem in a manner similar to that described in connection with FIGS. 1and 2A.

FIG. 2C is a plan view of yet another embodiment of a membrane unit. Inthis embodiment, the tubular membrane unit 195 comprises a tubularmembrane 196 that defines a cylindrical space 197 to hold a liquid. Apair of end caps 198 may be used to provide a liquid-tight seal at eachend of the tubular membrane 196. Each end cap may be connected to a pipeor tube 199 through which liquid may flow. In operation, a plurality ofthese tubular membrane units may be positioned parallel to one anotherin a structural support in a gas duct in any matrix arrangement desired.As shown, the tubular membrane units 195 can be oriented with theirlength parallel to the gas flow 210. Depending upon the operatingconditions, the liquid flow through the tubular membrane 196 may beco-current or counter-current to the gas flow 210.

In general, the membranes 140 are preferably polymer membranes. Thepolymer material should be selected based upon the vapor phasecontaminant being removed. For example, the porosity or permeability ofthe membrane should capable of allowing the sorbed vapor phasecontaminant, or any chemically altered form thereof, to be collected onor into the membrane and to pass through the membrane to the other side.Further, in some cases, it may be desirable to have the liquid that isheld in the region 170 between the membranes to permeate into themembrane, either partially or completely to the surface of the membrane,to assist with the sorption process. Therefore, the permeability of themembrane to the liquid that will be used in operation is also aconsideration. The overall gas conditions to which the polymer materialwill be exposed, such as temperature, corrosivity, acidity and thepresence of other gas components that may deleteriously affect themembrane integrity or performance, should also be taken into account inselecting the polymer material.

In one embodiment, the polymer membrane may comprise a permeable ionexchange membrane. Depending on the type of species to be removed fromthe gas stream, the polymer membrane may comprise either a permeableanion or a cation exchange membrane. With respect to mercury removal,the polymer membrane may comprise a permeable cation exchange membranebecause cationic forms of mercury are removed by the membrane removalsystem, as will be further described in connection with FIG. 5. Inconnection with the removal of sulfur oxides and nitrogen oxides, ananion exchange membrane may be used; however a cation exchange membranemay be used as well. Since ionic species may be formed upon the sorptionof a vapor phase contaminant, the polymer membrane should also functionas a solid polymer electrolyte in connection with the liquid occupied inthe region between the membranes.

In one embodiment, the membrane may comprise a perfluorinated polymer,such as DuPont's TEFLON®. In another embodiment, the polymer membranecomprises a perfluorinated polymer with an anionic functional group,such as sulfonic acid and carboxylic acid groups. For example DuPont'sNAFION® is a perfluorinated polymer with sulfonic acid functionalgroups. NAFION® has good chemical and thermal stability and an inherentability to act as a strong acid cation exchange material for sorbingsuch vapor phase contaminants such as mercury. Additionally, polymermembranes made of composites, such as a NAFION® and TEFLON® composite,may be used as well. Such membranes may also be used for removing sulfurand nitrogen oxides.

The thickness of the polymer membrane may vary. The polymer membraneshould be sufficiently thin to facilitate movement of the sorbedcontaminant, or any chemically altered form thereof, but should also beof sufficient structural integrity when exposed to the gas flow. Amembrane having a thickness of approximately 0.2 mm may be adequate formany applications. including, for example, use in a coal-fired boilerflue gas.

In another embodiment, the membrane 140 comprises a metallized membranethat can be used to assist with the sorption and chemical reaction orconversion of a given vapor phase contaminant once it is sorbed by themembrane to its desired reacted form. The metallized membrane maycomprise a metal layer disposed on its surface, which can be very thin,such as less than three microns. Alternatively, or in combination withthe metal layer, the metallized membrane may comprise metal particlesimpregnated into the membrane rather than being simply disposed on thetop surface of the membrane. The formation of a metallized membrane isdescribed below in connection with FIGS. 3 and 4.

The metal used can be selected from a variety of metals depending on thetype of vapor phase contaminant to be removed. For example, for somevapor phase contaminants, such as elemental mercury, it may be desirableto chemically convert the sorbed vapor phase contaminant to anotherform, in which case, the metal may act as a catalyst for this reaction.For example, it is desirable to oxidize sorbed mercury to an oxidizedform since it is more easily dissolved in the liquid on the other sideof the membrane. In this case, the ability of the metal to act as acatalyst in the oxidation process should be taken into account. Forexample, gold, silver, palladium, platinum, copper, nickel and mixturesthereof can be used when the vapor phase contaminant is mercury. Withrespect to elemental mercury removal, gold is a preferred metal becauseof mercury's affinity to gold and gold's ability to act as a catalyst inoxidizing elemental mercury.

Similarly, it may be desirable to oxidize sulfur dioxide into sulfuricacid, which may be readily dissolved into the liquid between themembranes. Ferric ion or manganese ion may be used as a metal catalystfor oxidizing sulfur dioxide and may be incorporated into the membranethrough the use of a ferric salt, such as ferric chloride or ferricsulfate, or through the use of a manganese salt, such as manganesesulfate or manganese chloride, respectively. With respect to NO, it maybe desirable to reduce the NO using dichromate or permanganate or byusing a complexing/reducing agent such as ferrousethylenediaminetetraacetic acid (ferrous EDTA).

It should be appreciated that other species may be incorporated into themembrane similarly to the above described metals. For example, Group VIelements may be used. Specifically, selenium may be used for mercuryoxidation. (It should be appreciated that all references to “metal,”“metal layer,” or “metallization” also encompass such other species thatmay be incorporated into the membrane, such as Group VI elements, suchas selenium.) It should be appreciated that carbon or activated carbonmay also be disposed on a membrane surface or within a membrane to whichvapor phase contaminants such as mercury may adsorb.

FIG. 3 is a flowchart of a method to produce a metallized membraneaccording to one embodiment of the present invention. Specifically, FIG.3 illustrates a manufacturing process 300 for producing a metallizedmembrane in which a metal layer is formed on the membrane surface.

In a first step 310, a polymer membrane is prepared so that the metallayer adheres to the polymer membrane's surface. In one embodiment, thepolymer membrane's surface is abraded to improve subsequent adhesion ofthe metal layer to that surface. This preparation step 310 may alsooptionally comprise boiling the polymer membrane in an approximate 6 Mnitric acid solution for approximately one hour, followed by boiling indeionized water for approximately one hour. It should be appreciatedthat depending upon the specific polymer membrane used, theconcentration of the nitric acid and the boiling times may be altered.

In a second step 320, the polymer membrane is mounted in a holderconfigured to separately hold two liquids, one on each side of themembrane. Depending on the size and geometry of the polymer membrane,the holder can be of any suitable size and geometry that can house thepolymer membrane. The holder can range from a filter holder to acustomized lank configured to receive a membrane that fluidly separatesthe tank into two compartments.

FIG. 3B is a perspective view of a tank used in the method of FIG. 3A.The tank 370 comprises a slot 390 configured to hold a membrane and tofluidly separate the tank 370 into two compartments 371, 372. FIG. 3C isa top view of a frame that may be used in connection with the tank ofFIG. 3B. The frame 391 may be used to hold the membrane 394 in astructurally sound position. The slot 390 may be configured to receivethe frame 391 such that the frame mates with the inside walls of thetank to fluidly separate the two compartments 371, 372. The tank 370 mayalso comprise a top or lid (not shown). In another embodiment, the tankmay be configured with a built-in gasket that separates the tank intotwo compartments and into which the membrane may be placed, without theneed for a separate frame. This tank may also comprise a top or lid witha corresponding gasket that mates with the top or exposed edge of themembrane. The holder should also have liquid inlet and drainage controlsand should be made of a material compatible with the liquids to be held.

In a third step 330, a first liquid is fed into one compartment of theholder, thereby contacting one side of the polymer membrane. This firstliquid comprises a chemical compound that has some form of the desiredmetal to be deposited on the side of the membrane, which will become themetallized surface. The form of the metal in this first liquid may be,for example, a reducible metal salt of the desired metal. In oneembodiment, this first liquid comprises a hydrogen tetrachloroaurate(HAuCl₄) solution to facilitate the deposition of a gold layer on themembrane, specifically an approximately 0.02 M HAuCl₄ solution. Asmentioned earlier, a gold-metallized membrane is preferred for mercuryremoval. In an alternative embodiment in which the resulting metal layercomprises palladium, the first liquid comprises a palladium chloridesolution. In another alternative embodiment in which the resulting metallayer comprises selenium, the first liquid comprises a potassiumselenocyanate solution (KSeCN). Further, a ferric salt, such as ferricchloride or ferric sulfate, may be used to generate a membranecomprising ferric ion, and a manganese salt, such as manganese sulfateor manganese chloride, may be used to generate a membrane comprisingmanganese ion. In addition, dichromate or permanganate or acomplexing/reducing agent such as ferrous ethylenediaminetetraaceticacid (ferrous EDTA) may be incorporated into the membrane in a. similarfashion.

In a fourth step 340, a second liquid is fed into the second compartmentof the holder, thereby contacting the other side of the polymermembrane. This second liquid comprises a chemical compound that canreduce the chemical compound of the first liquid described in the thirdstep 330. It should be appreciated that the side of the membrane that iscontacted by this second liquid will not have a metal layer disposedthereon. In the embodiment where the first liquid comprises a hydrogentetrachloroaurate (HAuCl₄) solution, the second liquid may comprise anapproximately 0.02 M hydrazine solution, in which the hydrazine solutionwould permeate across the polymer membrane to reduce the hydrogentetrachloroaurate solution on the other side of the polymer membrane,thereby producing a gold layer on the membrane surface that is incontact with the first liquid. It should be appreciated that improvedgold layer formation may occur through the addition of a salt, such assodium sulfate, to the hydrazine solution. In the embodiment where thefirst liquid comprises a palladium chloride solution, the second liquidmay also be an approximately 0.2 M hydrazine solution. In the embodimentwhere the first liquid comprises a potassium selenocyanate solution(KSeCN), the second liquid may be any acidic solution, such as HCl, thatwould acidify the potassium selenocyanate solution.

In a fifth step 350, the second liquid permeates through the polymermembrane, which reduces the first liquid, thereby forming a thinmetallic layer on the polymer membrane. Permeation of the second liquidoccurs over a period of time, ranging from approximately 20 minutes toapproximately 20 hours after the polymer membrane has been exposed tothe two liquids. The permeation time may be reduced by circulating thesecond liquid, rather than leaving it stagnant. Furthermore, thechemistry of the second liquid may also affect permeation time. Itshould be appreciated that while this process results in a metal layerprimarily on the surface of the membrane, metal may also be depositedwithin the membrane. The extent to which the metal is deposited withinthe membrane and below the surface of the membrane depends upon thepermeability of the membrane to the metal species in the solution, thetemperature, and the amount of time that the two liquids are in contactwith the membrane.

In the final step 360, the solutions are discharged from the holder andthe membrane is removed. At this point, the membrane is ready for use.It should be appreciated that in the embodiment where a frame is used tohold the membrane in the tank, this same frame may be used as the framethat holds the membrane in the membrane removal system or the structuralsupport for the membrane units.

In the case of producing a gold-metallized polymer membrane withhydrogen tetrachloroaurate and hydrazine according to the process 300described in FIG. 3, the gold in the hydrogen tetrachloroaurate solutionas described above should be nearly all consumed, which would naturallycomplete the process 300 because no more metallization can occur afterthe gold in the hydrogen tetrachloroaurate has been consumed. One way todetect the consumption of gold in hydrogen tetrachloroaurate is based onthe color of the hydrogen tetrachloroaurate solution, which istransformed from yellow to colorless as the gold is deposited on themembrane. Moreover, the resulting metal layer appears as a matte goldsurface on the metallized side of the polymer membrane. It should beappreciated that other metals or species may be incorporated into themembrane using this process.

It should also be appreciated that one of skill in the art can implementother methods of metal deposition, when producing a metallized membrane.For example, spray coating, spin coating, sputtering and electrolyticdeposition processes can be used to create a metal layer on a given sideof a polymer membrane. However, without being limited by theory, it isbelieved that the chemical reaction that occurs during the process 300described in FIG. 3 produces small metal particles on the membrane,which is more desirable for the purposes of the present inventionbecause the small particle size may provide more effective surface areafor sorbing the vapor phase contaminant.

FIG. 4 is a flowchart of a method to produce a metallized membraneaccording to another embodiment of the present invention. Morespecifically, this process 400 provides a method for producing ametal-impregnated polymer membrane. In a first step 410, a polymermembrane is soaked in a solution containing a reducible metal saltcomprising the metal to be impregnated into the membrane. The selectionof the reducible metal salt may also dictate the type of solvent that isused in creating the solution comprising the reducible metal salt. Ifthe metal salt is an anionic complex, then it would not permeate acationic exchange membrane because of its anionic sites, such as thesulfonic acid sites in NAFION®. For such cases, a solvent that minimizesdissociation of the metal salt should be used so that greaterpenetration of the metal Salt in an un-dissociated form is achieved. Inone embodiment, to produce a gold-impregnated polymer membrane, theNAFION® membrane is soaked for approximately one hour in an acetonitrilesolution containing approximately 50 mM AuCl at room temperature. Inanother embodiment, to produce a gold-impregnated polymer membrane, theNAFION® membrane is soaked for approximately one hour in a methanolsolution containing approximately 50 mM HAuCl₄ at room temperature.

In a second step 420, the polymer membrane is removed from the chemicalsolution used in the first step 410 and optionally cleaned. The cleaningof the membrane may comprise wiping, rinsing, blowing, or any othermeans known in the art to remove excess solution from the first step410. Some care should be exercised in the chemical removal and cleaningas to not introduce other gross contaminants, such as lint or dust.

In a third step 430, the polymer membrane is soaked in a reducing agent.The selection of the reducing agent depends on the chemistry of thesolution containing the reducible metal salt that was used in the firststep 410 and the composition of the polymer membrane. Generally, thepolymer membrane is exposed to the reducing agent for a period of timethat is relatively short, such as 10-30 minutes, as compared to theamount of time required to permeate the reducing solution through themembrane in the process 300 described in connection with FIG. 3.

In one embodiment for producing a gold-impregnated polymer membranethrough the use of the AuCl-acetonitrile solution, the NAFION® membraneis soaked in a solution of approximately 0.02 M hydrazine, which acts asthe reducing agent. Generally, this embodiment produces a black, opaquemembrane with colloidal gold particles dispersed within the membrane. Inanother embodiment for producing a gold-impregnated polymer membranethrough the use of the HAuCl₄-methanol solution, the NAFION® membrane issoaked for about 30 minutes in a solution of approximately 0.1 M sodiumborohydride (NaBH₄) and approximately 0.1 M sodium hydroxide (NaOH). Asknown in the art, sodium hydroxide may be substituted by potassiumhydroxide. Typically, this embodiment yields a pinkish transparent ortranslucent membrane with gold nanoparticles dispersed throughout themembrane.

In a final step 440, the membrane is either removed from the reducingagent solution or the solution is discharged from a container in whichthe membrane is soaking. At this point, the membrane is ready for use.

It should be appreciated that the process 400 described above in FIG. 4can be further varied to form other types of metal-impregnated membranesby using different reducible metal salts, solvents, reducing agents,polymer membrane and process conditions. For example, to form apalladium-impregnated NAFION® membrane, the NAFION® membrane may besoaked for approximately 30 minutes in an approximately 0.113 Mpalladium chloride (PdCl₂) solution at approximately 90° C. in the firststep 410, washed in water in the second step 420, and soaked in anapproximately 0.2 M hydrazine solution for 15 minutes in the third step430, which is then followed by another thorough water rinse. Theresulting palladium-impregnated NAFION® membrane is a dark membrane. Byvarying the reducible metal salts, solvents, reducing agents, polymermembrane and process conditions, especially temperature and exposuretime, the degree of metal impregnation into the membrane, both in termsof concentration of the metal in the membrane and the extent ofdispersion from one side of the membrane to the other, may be varied.

FIG. 5 is a flowchart of a method of vapor phase contaminant removalaccording to one embodiment of the present invention. This method 500 isgenerally a method for removing a vapor phase contaminant, such asmercury, from a gas stream, such as a flue gas stream comprising vaporphase contaminants such as, but not limited to, Hg, NO_(x) and SO_(x)that have been generated by a coal-fired power plant boiler, using anyof the embodiments of the membrane removal system described above.Moreover, it should be appreciated that the membrane removal system ofthe present invention may be capable of removing more than one vaporphase contaminant and may remove Hg, NO_(x) and SO_(x) together or inany combination. Therefore, it should be appreciated that the presentinvention is not limited to the removal of mercury from a flue gasstream and may be used to remove other vapor phase contaminants in thesame or in other types of gas streams. Regardless, the following methodis discussed in the context of mercury removal from flue gas generatedby a coal-fired power plant boiler; however, this description should notbe deemed limiting as to the application of the method to other vaporphase contaminants.

In a first step 510, a flue gas stream comprising mercury is directedthrough a duct in which is placed a membrane removal system according toany of the embodiments described herein. In a second step 520, the fluegas flows past the membrane removal system, thereby contacting thesurface of each membrane in each membrane unit in the membrane removalsystem. In one embodiment for use in removing mercury, the flue gas maycontact a bare membrane made of perfluorinated polymer containingsulfonic acid groups such as NAFION®. In another embodiment of thepresent invention, the flue gas stream may contact a metallizedmembrane, in which the metallized membrane comprises a polymer membrane,such as NAFION®, and a metal layer on the surface of the polymermembrane, where the metal layer may be gold. In yet another embodiment,the flue gas may contact a metal-impregnated polymer membrane, which mayalso comprise gold for use in mercury removal.

Again, it should be appreciated that depending upon the vapor phasecontaminant to be removed, different membranes and different types ofmetal for metallized membranes may be used or different compounds orspecies, such as carbon. For example, in removing sulfur oxides, such assulfur dioxide, a membrane having either a ferric ion- or manganeseion-based metal layer and/or having ferric ion or manganese iondispersed within the membrane may be used for oxidizing the sulfuroxide. In removing NO, a membrane having either a reducing agent such asdichromate or permanganate on or in the membrane may be used, or acomplexing/reducing agent such as ferrous ethylenediaminetetraaceticacid (ferrous EDTA) on or in the membrane may be used. It should beappreciated that membranes having a combination of the metals and/ormetal ions, for example, combinations of any of the metals and metalions described herein, may be used, including a combination of metalsand metal ions used in removing different vapor phase contaminants.

In a third step 530, the vapor phase contaminant in the flue gascontacts and is sorbed by the membrane. It should be appreciated thatthe sorption of the vapor phase contaminant may occur on the membrane'souter surface or the sorption may be below the outer surface of themembrane such that the vapor phase contaminant is sorbed into themembrane. In connection with the sorption of mercury, it should beappreciated that non-metallized NAFION® may be relatively effective insorbing mercury because the sulfonic acid sites in the membrane cancomplex mercury ions, which further facilitates mercury oxidation. Formore effective mercury sorption, a gold metallized membrane (either amembrane having a gold layer or a gold-impregnated membrane) may be usedsince mercury has a high affinity for gold and because gold has theability to collect all forms of mercury including elemental mercury,which is generally difficult to capture. Moreover, gold can be easilyapplied to a variety of membrane substrates. During the sorptionprocess, the sorbed mercury may amalgamate with the gold on the membranesurface to form amalgamated mercury.

In a fourth step 540, the sorbed vapor phase contaminant may be reactedto a more desired or reacted form, preferably one that is easilydissolved in the liquid in contact with the opposite side of themembrane. For example, sorbed mercury or amalgamated mercury on themembrane can be oxidized to an oxidized form of mercury by the oxygenpresent in the flue gas. This oxidation may be catalyzed by the membranematerial itself, such as NAFION®, and, in the case of a metallizedmembrane, by the metal on the membrane surface and/or by the metalpresent within the membrane. More specifically, elemental mercury, Hg⁰,may oxidize to a cationic form of mercury, such as Hg²⁺, and thisoxidation can be catalyzed by the metal, such a gold, that is present onand in the membrane. It should be appreciated that different chemicalreactions may be caused to occur, thereby chemically altering the formof a given sorbed vapor phase contaminant to further facilitate itsremoval from the membrane unit. For example, it may be desirable tochemically alter the form of a sorbed vapor phase contaminant tofacilitate its transport through the membrane or to enhance itssolubility in the liquid that flows between each pair of membranes in amembrane unit, thereby increasing the rate at which it is removed fromthe membrane. The composition of the membrane, the metal added to themembrane and the liquid, which will be further described, and possiblythe composition of the gas stream being treated (e.g., by the presenceof oxygen or other gaseous species), can be varied so that a givensorbed vapor phase contaminant can be reacted to produce a desiredchemical form that facilitates its removal. For example, in connectionwith the removal of sulfur dioxide, the sorbed sulfur dioxide may beoxidized to form sulfuric acid or sulfite and sulfate ions, which arereadily dissolvable in water, any aqueous solution, or an alkalinesolution. Similarly, sorbed nitrogen oxides may be reduced to formnitric acid, which is also readily soluble in water, any aqueoussolution, or an alkaline solution. As noted, in removing sulfur oxides,such as sulfur dioxide, a membrane having either a ferric ion- ormanganese ion-based metal layer and/or having ferric ion or manganeseion dispersed within the membrane may be used to oxidize the sorbedsulfur oxide. In removing NO, a membrane having either a reducing agentsuch as dichromate or permanganate on or in the membrane may be used, ora complexing/reducing agent such as ferrous ethylenediaminetetraaceticacid (ferrous EDTA) on or in the membrane may be used. It should beappreciated that membranes having a combination of the metals and/ormetal ions, for example, combinations of any of the metals and metalions described herein, may be used, including a combination of metalsand metal ions used in removing different vapor phase contaminants.

It should be appreciated that the liquid that flows between each pair ofmembranes in a membrane unit, which is discussed in more detail below inconnection with removing the sorbed vapor phase contaminant from themembrane unit, may also assist in chemically converting the sorbed vaporphase contaminant into a more desired form. For example, the liquidbetween each pair of membranes may permeate at least partially orcompletely into the membrane thereby coming in contact with the sorbedvapor phase contaminant. For example, if this liquid has the ability tooxidize, it may oxidize the sorbed vapor phase contaminant, therebyproviding additional oxidizing capacity in combination with thecatalytic facility provided by the membrane and metal as described aboveand the oxygen present in the flue gas. It should be appreciated that inthe case where the liquid fully permeates the membrane, that someevaporation of the liquid may occur. Therefore, liquid make-up may benecessary to the region between the membranes.

In the case of mercury removal, any suitable liquid can be used, as longas it can oxidize mercury. For example, ferric chloride, potassiumpermanganate and hydrogen peroxide are suitable oxidizing liquids. Inone embodiment, nitric acid may be used as the oxidizing liquid.Additionally, the oxidizing liquid may be combined with a complexingagent for oxidized mercury, such as Hg²⁺, which may further facilitatethe transport and removal of the mercury from the membrane. Suchcomplexing agents may include chlorides, ethylenediaminetetraacetic acid(EDTA), iodide and sulfur or sulfur compounds, such as ones containingsulfides or alkylthiol. In the case of the removal of sulfur oxides ornitrogen oxides, water, any aqueous solution, or any alkaline solutionmay provide a suitable liquid for use between the membranes fordissolving the sorbed vapor phase contaminant or its chemically alteredform.

Further, in the case of mercury removal, as a result of oxidizing theamalgamated mercury, the gold metal is regenerated. Without beinglimited to theory, it is believed that once the mercury is oxidized orconverted into a cationic form, it is released by the gold metal fortransport through the membrane, thereby regenerating the gold in themetal layer.

In a fifth step 550, the sorbed vapor phase contaminant, or its reactedor chemically altered form, is transported through the membrane to theside that is in contact with the liquid that flows between each pair ofmembranes in a membrane unit. As noted above, the membrane compositionand its thickness should be conducive to the transporting and diffusionof the sorbed vapor phase contaminant or its chemically altered form,such as cationic mercury. For example, the membrane should besufficiently permeable to handle cationic mercury. Further, a membranethat is too thick may impede the movement of cationic mercury within themembrane. On the other hand, a membrane that is too thin may be suitablefor transporting of cationic mercury but may be mechanically weaker anddegrade faster over time, thereby requiring more frequent replacement.In one embodiment, a NAFION® membrane having a thickness ofapproximately 0.2 mm provides sufficient molecular movement or diffusionthrough the membrane and good mechanical or structural integrity.

In a sixth step 560, the sorbed vapor phase contaminant, or itschemically altered form, is dissolved or absorbed into the liquid thatflows between each pair of membranes in a membrane unit. It should beappreciated that the contaminant or its chemically altered form mayactually be dissolved or absorbed into the liquid after it has beentransported through the membrane, or it may be dissolved or absorbedinto liquid that has permeated the membrane. Once the sorbed contaminantor its chemically altered form is present in this liquid, it can betransported out of the membrane unit and membrane removal system and outof the duct.

A variety of chemicals may be used as the liquid that flows between eachpair of membranes, and the choice depends on the type of vapor phasecontaminant to be removed, the polymer membrane material, the metal usedin conjunction with the membrane and its regenerability and the desiredremoval rate of the vapor phase contaminant. Generally, the liquidshould be capable of dissolving or absorbing the vapor phase contaminantor its chemically altered form, so that the vapor phase contaminant maybe removed from the metallized membrane surface and subsequently fromthe membrane removal system and the gas duct. In addition, chemicalcompatibility and concentration of the liquid needs to be consideredwith respect to the polymer membrane material and any metal used inconjunction with the membrane to minimize or avoid any degradation ofthe membrane. Generally, the liquid will be water-based, althoughnon-aqueous solvents may be applied, such as propylene carbonate.

It should be appreciated that the liquid may comprise a solution havingvarious chemical species that assist in chemically converting a sorbedcontaminant to a more desired form. For example, the liquid may containspecies that facilitate oxidation of the sorbed contaminant to anoxidized form, a cationic form or an anionic form. In this case, theselection of an oxidizing liquid may be based upon the oxidationpotential of the sorbed contaminant. Alternatively, if a metal is usedin conjunction with the membrane that provides sufficient catalysis foroxidation by other system components, the liquid may not need to becapable of oxidizing the sorbed contaminant. Examples of suitablechemicals for use in a water-based solution for this liquid includenitric acid, ferric chloride, ferric citrate, ferric thiocyanate, ferricnitrate, a combination of ferric chloride and sodium citrate, potassiumpermanganate, potassium iodide, iodine, a combination of potassiumiodide and iodine, a combination of potassium iodide, iodine andpropylene carbonate, methylene blue, polyaniline, hydrogen peroxide andhypochlorite. Water by itself may also be a suitable liquid for thisstep. Furthermore, potassium- and sodium-based compounds with the sameanionic species are often interchangeable with one another. For examplepotassium iodide can be substituted for sodium iodide and vice versa. Inthe case of mercury removal, preferred embodiments of the liquid includenitric acid, a nitric acid solution with a complexing agent for oxidizedmercury such as Hg²⁺, and ferric chloride. Suitable complexing agentsfor oxidized mercury include chlorides, ethylenediaminetetraacetic acid(EDTA), iodide and sulfur or sulfur compounds, such as ones containingsulfides or alkylthiol. In the case of the removal of sulfur oxides ornitrogen oxides, water, any aqueous solution, or any alkaline solutionmay provide a suitable liquid for use between the membranes fordissolving the sorbed vapor phase contaminant or its chemically alteredform.

Since the liquid affects removal of the vapor phase contaminant, and mayaffect any reaction of the sorbed contaminant to form a more desiredform, as well as the regeneration of any metal used in conjunction withthe membrane, the membrane unit should be constructed to either providea sufficient volume of liquid between each pair of membranes or asufficient flow of fresh liquid between the membranes. Generally, thedistance between a pair of membranes may be approximately 1-3centimeters or less. Regardless of the volume between each pair ofmembranes, the flow rate of the liquid through this region may also beoptimized to provide enough driving force for the dissolution orabsorption of the sorbed contaminant or its chemically altered form intothe liquid, as discussed below.

In the seventh step 570, the liquid between the membranes is removedfrom the membrane units in the membrane removal system and either freshor regenerated liquid is fed to the membrane units. This may beaccomplished using a recirculation system wherein the liquid beingremoved from the membrane units (spent liquid) is sent to a regenerationsystem where the sorbed contaminant is removed from the liquid and theliquid is regenerated and returned to the membrane units on a continuousbasis. The spent liquid may be regenerated by oxidation or otherchemical or electrochemical process that restores the liquid's abilityto dissolve the sorbed contaminant.

Alternatively, spent liquid may simply be discharged from the membraneunits, and fresh liquid may be fed to the membrane units on a continuousor semi-continuous basis depending upon the removal rate of thecontaminant(s) from the gas. Alternatively, the liquid may be dischargedand fresh liquid fed to the membrane units batch-wise in intervalsdictated by the need for fresh liquid, which would depend upon theamount of vapor phase contaminant absorbed by the liquid and thecapacity of the liquid for that contaminant. In yet another embodiment,the membrane units may be constructed such that the liquid is notremovable from between the membranes and once spent, the entire membraneunit may simply be replaced.

Having described the process generally for use of the membrane removalsystem for the removal of vapor phase contaminants, it should beappreciated that in the context of mercury removal from the flue gas ofa coal-fired boiler, it is desirable to utilize metallized membranesmade of a perfluorinated polymer with sulfonic acid groups, such asNAFION®, wherein the metal comprises a gold metal layer or goldparticles impregnating the membrane. The liquid between the metallizedmembranes may be a solution of nitric acid, a nitric acid solution witha complexing agent for oxidized mercury, a solution of ferric chloride,a solution of ferric thiocyanate, or a solution of ferric citrate. Inaddition, the liquid between a gold-impregnated polymer membrane mayalso be water.

The following Examples are provided as illustrative only and are notintended to limit to the scope of the invention.

EXAMPLE 1

Bench-scale experiments were performed using metallized NAFION® 117membranes and a non-metallized NAFION® 117 membranes, which is a0.007-inch thick clear plastic sheet with good mechanical properties.The metallized membranes further comprised a gold-layered membrane and agold-impregnated membrane, which included both colloidal gold particlesand gold nanoparticle varieties. For comparison, bench-scale experimentswere also performed using a gold-plated 18 gauge stainless steel screen.

Simulated flue gas contacted one side of each membrane, and liquid waspresent on the opposite side of the membrane. The flue gas flow rate was1.0 L/minute, which produced a linear velocity of 1.4 ft/sec flue gasacross the membrane surface. The liquid flowed continuously over the wetside of the membrane at a flow rate of 1.34 minute using a peristalticpump. The reactor and liquid were kept in an insulated and thermostattedoven maintained at 130° F. The tests lasted between 20 to 40 hours.

The simulated flue gas composition comprised a mixture of nominally 400ppm SO₂, 200 ppm NO_(x), 2 ppm HCl, 6% O₂, 12% CO₂, 7% H₂O, balance N₂.Moisture was added to the reaction gas by flowing a known volume ofnitrogen gas through a temperature-controlled saturator. Mercury wasadded to the gas by flowing a nitrogen carrier stream through atemperature-controlled permeation chamber containing elemental mercury.The nominal inlet mercury concentration was 37 microgram/Nm³. The gases,water vapor, and nitrogen stream containing mercury were mixed in amixing tube and directed to the membrane.

During each test mercury concentrations were measured. To ensureaccurate measurements, the reactor outlet gas stream was sent through aliquid gas conditioning system before reaching the analytical system toremove the acid gases from the gas stream and to convert all of themercury species to an elemental form. Gas phase mercury was thenmeasured semi-continuously using a gold amalgamation unit followed bythe CVAA (cold-vapor atomic absorption) unit. Inlet mercuryconcentrations were measured before and after each test, and outletconcentrations were monitored during each test.

Table 1 summarizes the results of these experiments.

TABLE 1 Maximum Hg⁰ Average Hg⁰ SO₂* Absorption Absorption Removal (% ofinlet (% of inlet (mM Membrane Liquid Time (hours) Hg⁰) Hg⁰) sulfate)Gold-layered 2.0 M 21.7 85 60 6.5 NAFION ® nitric acid Colloidal 2.0 M21.7 83 60 6.9 gold- nitric acid impregnated NAFION ® Nano-particlewater 40 40 30 — gold- impregnated NAFION ® Bare 2.0 M 21.7 35 15 1.6NAFION ® nitric acid Gold-plated 2.0 M 20 34 7.8 — 18 gauge nitric acidstainless steel screen *SO2 removal is indicated by the presence ofsulfate as measured in the liquid.

EXAMPLE 2

Additional experiments on NAFION® membranes were performed underconditions similar to Example 1, to evaluate various liquids. Table 2summarizes the results of these experiments.

TABLE 2 Elemental mercury absorption by Nafion 117 (except as noted)with different liquids. Average Hg° Liquid Absorption (%) H₂O 6.3 2.0 MHNO₃ 15.0 1.0 M Ferric Chloride 23.0 1.0 M Ferric Nitrate 0.0 0.1 MFeCl₃ + 0.2 M Na₃ Citrate 14.0 0.5 M Potassium Ferricyanide 1.2 0.05 MMethylene Blue 4.6 1.0 M KI + 0.1 M I₂ 69.0 1.0 M KI + 0.02 M I₂ 55.01.0 M KI + 0.02 M I₂ with 0.09 mm Nafion 27.0 5.0 M KI + 0.05 M I₂ 47.50.625 M KI + 0.0625 M I₂ in H₂O-saturated propylene carbonate 16.2

While the foregoing description represent various embodiments of thepresent invention, it should be appreciated that the foregoingdescription should not be deemed limiting since additions, variations,modifications and substitutions may be made without departing from thespirit and scope of the present invention. It will be clear to one ofskill in the art that the present invention may be embodied in otherforms, structures, arrangements, and proportions and may use otherelements, materials and components. For example, although the method isdescribed in connection with the removal of mercury from a flue gasstream, the method can be adapted for the removal of other vapor phasecontaminants by varying the polymer membrane composition, the metal usedin conjunction with the membrane, and the composition of the liquid thatis used between each pair of membranes. Moreover, it should beappreciated that different membrane units comprising different membranesor metallized membranes and different liquids may be used together inthe same membrane removal system to remove more than one type of vaporphase contaminant. The present disclosed embodiments are, therefore, tobe considered in all respects as illustrative and not restrictive, thescope of the invention being indicated by the appended claims and notlimited to the foregoing description.

1. An apparatus for removing mercury from a gas stream flowing in a gasduct, comprising: a membrane disposed within a gas duct; and a containerconfigured to hold a liquid adjacent to a first side of said membrane 2.A method for producing a metallized membrane, comprising: contacting afirst side of a polymer membrane with a first solution comprising ametal; contacting a second, opposite side of said polymer membrane witha second solution comprising a reducing solution; and passing saidreducing solution through said polymer membrane, thereby reducing saidfirst solution and depositing said metal on said first side of saidpolymer membrane.